Process and apparatus for ammonia synthesis gas production

• US 4,592,860 A
• Filed: 02/07/1984
• Issued: 06/03/1986
• Est. Priority Date: 02/07/1984
• Status: Expired due to Fees

• Current Assignee: UOP Des Plaines IL A NY General Partnership
• Original Assignee: Union Carbide Corporation (Dow, Inc.)
• Inventors: Fuderer, Andrija
• Primary Examiner(s): Trousof, Natalie
• Assistant Examiner(s): Gray, Bruce D.
• Application Number:
  US06/577,836
• Time in Patent Office: 847 Days
• Field of Search: 252/373, 252/376, 252/375
• US Class Current: 252/376
• CPC Class Codes: C01B 3/025 Preparation or purification of gas mixtures for ammonia synthesis
• CPC Class Codes: Y02P 20/129 Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Abstract

A fluid hydrocarbon feed stream is converted with excess air to a mixture of hydrogen and carbon monoxide, also containing the nitrogen content of said air. Following high temperature shift conversion to convert said carbon monoxide to hydrogen and carbon dioxide, the gas mixture is passed to a pressure saving adsorption system used to produce an impure ammonia synthesis gas mixture of hydrogen and nitrogen, with excess nitrogen being separated and removed therefrom with the impurities discharged from the system at high operating pressures, the purge gas effluent from the pressure swing adsorption system can be passed to an expansion turbine for desirable power energy. The ammonia synthesis gas, which can be passed to a methanator for final purification, is thus produced without the need for employing an air separation plant or a nitrogen plant.

Claims

1. An improved process for the production of ammonia synthesis gas comprising:

(a) catalytically reacting a hydrocarbon feed stream with steam in a primary reforming unit to form a primary reformed gas mixture containing hydrogen and carbon monoxide;

(b) passng said primary reformed gas mixture to a secondary reforming unit for reaction of unconverted methane present therein with air, the amount of said air introduced to said secondary reforming unit being considerably in excess of that required to furnish the stoichiometric amount of nitrogen required for reaction with hydrogen for said ammonia synthesis;

(c) subjecting said secondary reformed gas mixture to water gas shift conversion to convert most of the carbon monoxide present in said reformed gas mixture to hydrogen and carbon dioxide;

(d) passing the thus-shifted gas mixture containing hydrogen, carbon dioxide, residual carbon monoxide, methane, argon and said excess nitrogen, without necessary treatment for removal of a major portion of the carbon dioxide content thereof and without methanation to remove carbon oxides to low levels, to a pressure swing adsorption system capable of selectively adsorbing carbon dioxide, carbon monoxide, methane and other impurities from said hydrogen and from a portion of said nitrogen present in the gas passed to said system, the processing cycle in the pressure swing adsorption system comprising;

(i) introduction of the thus-shifted gas mixture to the inlet end of an adsorbent bed at an adsorption pressure level, with adsorption of impurities therefrom and discharge of a partially purified ammonia synthesis gas mixture of hydrogen and nitrogen from the discharge end thereof, excess nitrogen being adsorbed in the adsorbent bed;

(ii) partial cocurrent depressurization of the adsorbent bed with release of hydrogen-containing void space gas from the discharge end of the bed upon being displaced by desorbed nitrogen, the nitrogen peak in the bed, being rolled up by the trailing adsorbed carbon dioxide front, then being pushed out of the discharge end of the bed, said nitrogen being used to provide purge gas to another adsorbent bed in the system;

(iii) countercurrent depressurization of the bed with release of gas from the inlet end thereof, thereby depressurizing the bed to its lower desorption pressure;

(iv) introduction of purge gas comprising desorbed nitrogen to the discharge end of the bed at its lower desorption pressure level, with discharge of purge gas effluent from the inlet end of the bed;

(v) repressurization of the purged bed to said adsorption pressure level; and

(vi) repetition of said cyclic steps (i)-(v) with additional quantities of the thus-shifted gas mixture, whereby excess nitrogen present in the reformed gas mixture being treated is conveniently used in the pressure swing adsorption system as purge gas and high hydrogen recoveries can be obtained, and the desired ammonia synthesis gas is produced without a requirement for employing an air separation or nitrogen plant to provide the nitrogen content of said ammonia synthesis gas.

2. the process of claim 1 in which the purge gas effluent discharged from the inlet end of the bed is at a pressure of from about 60 to about 100 psia.

3. The process of claim 2 and including expanding said purge gas effluent discharged from the inlet end of the bed in an expansion turbine, thereby generating power and further enhancing the overall ammonia synthesis process.

4. The process of claim 3 in which said purge gas effluent is preheated and/or combusted with air and is expanded to about atmospheric pressure.

5. The process of claim 4 in which said purge gas effluent discharged from the inlet end of the bed is at a pressure of from about 70 to about 80 psia.

6. The process of claim 4 and including passing said expanded purge gas to said primary reforming unit for use as fuel therein.

7. The process of claim 4 in which said thus-shifted gas mixture passed to the pressure swing adsorption system contains excess nitrogen such that the hydrogen-nitrogen molar ratio thereof is between about 1/1 and about 2.4/1. and shift conversion consisting of high temperature shift only.

8. The process of claim 7 in which the ammonia synthesis gas mixture discharged from the pressure swing adsorption system contains essentially 75% hydrogen and 25% nitrogen, together with minor amounts of carbon monoxide, methane and argon.

9. The process of claim 1 in which the air passed to said secondary reforming unit is at a pressure of from about 500 to about 1000 psia.

10. The process of claim 9 in which said pressure is from about 700 to about 900 psia.

11. The process of claim 1 and including diverting a portion of the fluid hydrocarbon feed stream passing to the primary reforming unit for passage directly to said secondary reforming unit, thereby achieving a significant reduction in the steam requirements for said primary reforming unit.

12. The process of claim 11 and including recovering heat from the secondary reformed gas mixture prior to subjecting said mixture to shift conversion.

13. The process of claim 12 and including water quenching said secondary reformed gas mixture for temperature reduction thereof prior to said recovery of heat from said gas mixture.